|本期目录/Table of Contents|

[1]康海南,朱赫礼,罗毅.国产加氢催化剂HYT-6319及HC-185 LT/HC-53 LT的工业应用[J].石化技术与应用,2024,2:129-133.
　KANG Hai-nan,ZHU He-li,LUO Yi.Industrial application of domestic HYT-6319 and HC-185 LT/HC-53 LT hydrogenation catalysts[J].Petrochemical technology & application,2024,2:129-133.
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国产加氢催化剂HYT-6319及HC-185 LT/HC-53 LT的工业应用(PDF)

《石化技术与应用》[ISSN:1009-0046/CN:62-1138/TQ]

期数:
2024年2期
页码:
129-133
栏目:
出版日期:
2024-03-10

文章信息/Info

Title:
Industrial application of domestic HYT-6319 and HC-185 LT/HC-53 LT hydrogenation catalysts
文章编号:
1009-0045（2024）02-0129-05
作者:
康海南; 朱赫礼; 罗毅
中国石油广东石化公司 炼油生产三部，广东 揭阳 515299
Author(s):
KANG Hai-nan; ZHU He-li; LUO Yi
3rd Refinery Production Department of Guangdong Petrochemical Company，PetroChina，Jieyang 515299，China
关键词:
加氢裂化; 加氢精制; 催化剂; 柴油; 航空煤油; 重石脑油; 收率
Keywords:
hydrocracking;  hydrorefining;  catalyst;  diesel oil;  aviation kerosene;  heavy naphtha; yield
分类号:
TE 624.9+3
DOI:
DOI：10.19909/j.cnki.ISSN1009-0045.2024.02.0129
文献标识码:
B
摘要:
在中国石油广东石化公司370万t/a加氢裂化装置中，以中质减压蜡油和重芳烃的混合油（二者质量比97∶3）为原料，使用经UOP公司授权由中国石油抚顺石化公司生产的加氢精制催化剂HYT-6319和加氢裂化催化剂HC-185 LT/HC-53 LT进行了工业应用，考察了催化剂运行情况、产品性质及其分布。结果表明：在催化剂运行中，一段精制、一段裂化、二段裂化反应器各床层入口平均温度依次比设计值低23.5~38.7，22.8~25.0，34.3~44.9 ℃，一段精制反应器床层平均温升比设计值低10.1 ℃，一段裂化、二段裂化反应器床层平均温升比设计值分别高3.4，3.6 ℃；柴油和航空煤油产品均满足国Ⅵ标准，重石脑油含硫（氮）量均小于0.5 μg/g，是优质的重整装置原料，轻石脑油含硫量为2.8 μg/g，是优质的乙烯裂解原料；主要产品重石脑油、航空煤油、轻石脑油、柴油的收率依次为48.62%，25.28%，5.47%，14.14%，产品总收率为93.51%，比设计值高0.04个百分点。
Abstract:
In the 3.70 Mt/a hydrocracking unit of Guangdong Petrochemical Company of PetroChina， a mixture of medium quality vacuum wax oil and heavy aromatics （with the mass ratio of 97∶3） was used as raw oil. The hydrofining catalyst HYT-6319 and hydrocracking catalyst HC-185 LT/HC-53 LT produced domestically by Fushun Petrochemical Company of PetroChina and authorized by UOP Company were used for industrial application. The catalysts operation， product properties and distribution were investigated. The results showed that during the operation of the catalysts， the average temperature at the inlet of each bed layer in the first refining， first cracking， and second cracking reactors was lower than the design value by 23.5-38.7，22.8-25.0，34.3-44.9 ℃， respectively. The average temperature rise of the bed layer in the first refining reactor was lower than the design value by 10.1 ℃， and the average temperature rise of the bed layer in the first cracking and second cracking reactors was higher than the design value by 3.4，3.6 ℃， respectively. Both diesel and aviation kerosene products met the national Ⅵ standard， and the sulfur （nitrogen） content of heavy naphtha was less than 0.5 μg/g and being a high-quality raw material for reforming units. The sulfur content of light naphtha was 2.8 μg/g and being a high-quality ethylene cracking raw material. The yield of the main products including heavy naphtha， aviation kerosene， light naphtha，and diesel was 48.62%， 25.28%， 5.47%， and 14.14%， respectively. The total yield of product was 93.51%. It was higher than the design value by 0.04 percentage points.

参考文献/References

［1］ 方向晨.加氢裂化工艺与工程［M］.2版.北京：中国石化出版社，2021：101.［2］ 沈本贤.石油炼制工艺学［M］.2版.北京：中国石化出版社，2022：305.［3］ 郝文月，刘昶，曹均丰，等.加氢裂化催化剂研发新进展［J］.当代石油石化，2018，26（7） ： 29-34.［4］ 周厚峰，张慧汝，田梦，等. 加氢裂化催化剂研究进展［J］.工业催化，2014，22（10）：729-735.［5］ 孙建怀.加氢裂化装置技术问答［M］.2版.北京：中国石化出版社，014：73-74.［6］ 杨洋.加氢裂化催化剂硫化的研究［J］.山东化工，2015，44（ 20） ： 38-39.［7］ 方向晨.加氢裂化工艺与工程［M］.2版.北京：中国石化出版社，2021：1041.

备注/Memo

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更新日期/Last Update: 2024-03-10